Plasma gasification reactors with modified carbon beds and reduced coke requirements

ABSTRACT

An apparatus includes a reactor vessel containing a carbonaceous bed and having means for establishing an elevated temperature within the carbonaceous bed; and the reactor vessel also having one or more feed material inlets above the carbonaceous bed for depositing process material from outside the vessel onto the carbonaceous bed, one or more gas exhaust ports above the bed for exit of gaseous products from the vessel, and one or more slag ports at the bottom of the carbonaceous bed for exit of molten and vitreous material from the vessel; wherein the carbonaceous bed comprises bricks that contain carbon and are of varied size and shape of which at least 25% of the total carbon content of the bed comprises spent pot liner material from aluminum processing, and wherein the bricks further comprise at least one of: Portland cement, potassium silicate cement, or aluminum silicate cement.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a divisional application of U.S. patent applicationSer. No. 13/199,814, titled “Plasma Gasification Reactors With ModifiedCarbon Beds And Reduced Coke Requirements”, filed Sep. 9, 2011, whichclaims the benefit of U.S. Provisional Application No. 61/403,123, filedSep. 11, 2010. Both of these applications are hereby incorporated byreference.

U.S. patent application Ser. No. 13/199,813, by some of the presentinventors and others and assigned to the same assignee as the presentapplication, titled “Enhanced Plasma Gasifiers for Producing Syngas,”includes descriptions of plasma reactors and their operation combinablewith the subject matter of the present application and is herebyincorporated by reference for such descriptions.

FIELD OF THE INVENTION

The invention relates to reactors that can be applied for gasificationor vitrification of a wide variety of materials and which have reactionbeds of carbonaceous material. Plasma gasification reactors are one formof such reactors to which the invention may be applied.

BACKGROUND

Plasma gasification reactors (sometimes referred to as PGRs) are a typeof pyrolytic reactor known and used for treatment of any of a wide rangeof materials including, for example, scrap metal, hazardous waste, othermunicipal or industrial waste and landfill material, and vegetativewaste or biomass to derive useful material, e.g., metals, or a synthesisgas (“syngas”), or to vitrify undesirable waste for easier disposition.In the present description, “plasma gasification reactor” and “PGR” areintended to refer to reactors of the same general type whether appliedfor gasification or vitrification, or both. Unless the context indicatesotherwise, terms such as “gasifier” or “gasification” used herein can beunderstood to apply alternatively or additionally to “vitrifier” or“vitrification”, and vice versa.

PGRs and their various uses are described, for example, in IndustrialPlasma Torch Systems, Westinghouse Plasma Corporation, DescriptiveBulletin 27-501, published in or by 2005; a paper by Dighe inProceedings of NAWTEC16, May 19-21, 2008, (Extended Abstract#NAWTEC16-1938) entitled “Plasma Gasification: A Proven Technology”; apaper of Willerton, Proceedings of the 27^(th) Annual InternationalConference on Thermal Treatment Technologies, May 12-16, 2008, sponsoredby Air & Waste Management Association entitled “PlasmaGasification—Proven and Environmentally Responsible” (2008); U.S. Pat.No. 7,632,394 of Dighe et al., issued Dec. 15, 2009, entitled “Systemand Process for Upgrading Heavy Hydrocarbons”; a U.S. patent applicationof Dighe et al., Ser. No. 12/157,751, filed Jun. 14, 2008, entitled“System and Process for Reduction of Greenhouse Gas and Conversion ofBiomass”, (Patent Application Publication No. 2009/0307974, Dec. 17,2009), and Dighe et al. patent application Ser. No. 12/378,166, filedFeb. 11, 2009, entitled “Plasma Gasification Reactor”, (PatentApplication Publication No. 2010/0199557, Aug. 12, 2010), all of saiddocuments being incorporated by reference herein for their descriptionsof PGRs and methods practiced with them.

It is known to set up and operate such PGRs with a carbonaceous bed in alower part of a reactor vessel where the bed is arranged with plasmatorches that elevate the bed temperature (e.g., to at least about 1000°C.) for thermal reaction with added material that is to be gasified orvitrified. Although there have been suggestions that carbon material forsuch a carbonaceous bed can be of a variety of carbon bearing materials,there has in the past been a heavy reliance on the use of coke for suchpurposes as it is about 90% pure carbon and has chemical, thermal, andstrength properties that are favorable for many processes that areperformed in such reactors. “Coke” is a term for a product of a fossilfuel e.g., coal or petroleum, subjected to drying, e.g., by baking, todrive off volatile constituents.

While the carbonaceous bed is an important component in the operation ofa PGR, another known form of a gasification reactor is a gasifierutilizing a carbonaceous bed (of coke) but without utilizing plasmatorches. The carbonaceous bed of such a reactor serves all the samefunctions as it does in a PGR with respect to the distribution of gasesand the movement of molten materials. However, in addition, thecarbonaceous bed also serves to provide the thermal energy forgasification that would otherwise be provided by a plasma torch. Acarbonaceous bed of such a reactor may be initially activated to atemperature for gasification by, for example, brief ignition of naturalgas supplied to the bed.

Among the desirable criteria of the carbonaceous bed of PGRs and otherreactors is that it be of particles irregular enough in shape to leavevoids allowing gases to flow to the surface of the particles wherereactions occur and gaseous reaction products to rise from the bed. Thevoids also allow molten metals and other liquids resulting from theprocess performed in the reactor to flow down to a metal and slag exitport. Voids of the bed and the porosity of particles of the bed cancontribute to desirable reactions and flow characteristics. Coke allowsthe formation of such a bed and has sufficient strength of the particlesfor many processes not to be crushed during operation by the burden ofworking material deposited on top of the bed.

Despite the satisfactory performance that coke very often provides, itis sometimes the case that factors such as the expense of coke andconcerns about its manufacture and use impacting the environment, as itis a fossil fuel, may prevent or limit its use in some processes at somereactor sites.

Known prior art, U.S. Pat. No. 4,828,607 issued May 9, 1989, to Dighe etal., and entitled “Replacement of Coke in Plasma-Fired Cupola”,discloses a process that includes providing coal instead of coke,although still a fossil fuel, along with metal scrap and a fluxingmaterial, to a plasma-fired cupola to produce iron or ferro-alloys. Thisevidences fairly early interest in minimizing coke usage in suchapplications although coke still remains the only form of carbonmaterial that is widely used in operating reactors with carbonaceousbeds. Wood or wood products (e.g., charcoal) are known carbon sourcesbut have not found practical application as significant cokereplacements in pyrolytic reactors.

SUMMARY

In one embodiment, an apparatus includes a reactor vessel containing acarbonaceous bed and having means for establishing an elevatedtemperature within the carbonaceous bed; and the reactor vessel alsohaving one or more feed material inlets above the carbonaceous bed fordepositing process material from outside the vessel onto thecarbonaceous bed, one or more gas exhaust ports above the bed for exitof gaseous products from the vessel, and one or more slag ports at thebottom of the carbonaceous bed for exit of molten and vitreous materialfrom the vessel; wherein the carbonaceous bed comprises bricks thatcontain carbon and are of varied size and shape of which at least 25% ofthe total carbon content of the bed comprises spent pot liner materialfrom aluminum processing, and wherein the bricks further comprises atleast one of: Portland cement, potassium silicate cement, or aluminumsilicate cement.

In another embodiment an apparatus includes a reactor vessel containinga carbonaceous bed and having means for establishing an elevatedtemperature within the carbonaceous bed; and the reactor vessel alsohaving one or more feed material inlets above the carbonaceous bed fordepositing process material from outside the vessel onto thecarbonaceous bed, one or more gas exhaust ports above the bed for exitof gaseous products from the vessel, and one or more slag ports at thebottom of the carbonaceous bed for exit of molten and vitreous materialfrom the vessel; wherein the carbonaceous bed comprises bricks thatcontain carbon and are of varied size and shape of which at least 25% ofthe total carbon content of the bed comprises soot water residue from agasification reactor, and wherein the bricks further comprises at leastone of: Portland cement, potassium silicate cement, or aluminum silicatecement.

In another embodiment an apparatus includes a reactor vessel containinga carbonaceous bed and having means for establishing an elevatedtemperature within the carbonaceous bed; the reactor vessel also havingone or more feed material inlets above the carbonaceous bed fordepositing process material from outside the vessel onto thecarbonaceous bed, one or more gas exhaust ports above the bed for exitof gaseous products from the vessel, and one or more slag ports at thebottom of the carbonaceous bed for exit of molten and vitreous materialfrom the vessel; and additional inlets through the side wall of thereactor vessel for injection of carbon fines into the carbonaceous bedwherein the additional inlets include at least one inlet that isarranged to receive carbon fines from an arrangement that includes aneductor receiving a carrier gas of solids at a first pressure and apressurized gas at the second, higher, pressure injecting solids fromthe first gas into the carbonaceous bed.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is an elevation view, partly in section, of an example of aplasma gasification reactor in accordance with an embodiment of theinvention.

FIG. 2 is a partial elevation view of an example of a carbonaceous bed.

FIG. 3 is an elevation view of an example of a bed with non-coke woodblocks.

FIG. 4 is an elevation view of an example of a bed with non-cokecarbonaceous bricks.

FIG. 5 is a block diagram of a system that is one example of the use ofnon-coke carbon in a PGR.

FIG. 6 is a partial, sectional, elevation view of a PGR with an exampleof a plate or grid supporting a charge bed.

FIGS. 7A and 7B are, respectively, elevation and plan views of anexample of a PGR with feed chutes at or near the top of a charge bed.

FIG. 8 is a schematic diagram of an example of a system for injectingparticles or fines into a carbon bed of a gasifier.

DETAILED DESCRIPTION

In various embodiments, the invention provides, in various forms and byvarious processes, reactors and carbonaceous beds that require less cokethan has been generally the case in the past. The carbon required can beobtained, at least in part, by carbon bearing alternatives to coke.Examples include beds that have at least about 25% (it can besignificantly greater up to 100%) of the carbon content of the bed madeof non-coke units that may be either, or both, wood blocks of naturalwood or bricks comprising carbon-containing particles or fines and oneor more binders and possibly a catalyst. Any such materials may beapplied in a bed also including coke (although coke may be replacedcompletely in some applications). Carbon of the bed may additionallyinclude, if desired, for example, if included in feed material to thecarbonaceous bed, other non-coke materials such as raw coal (anthraciteor bituminous), charcoal, or process materials including biomass (anycarbon bearing materials).

Some embodiments of the invention take advantage of, and make use of,carbon material resulting as waste from any of a variety of otherprocesses (e.g., carryover from any gasification reactor, fly ash fromcoal fired boilers, as well as others) which contribute to lesseningrequirements for coke in the bed. For one thing, they may beadvantageously used as particles or fines in making the above-mentionedbricks. Such waste carbon materials may also be included in the feedstock to the reactor without being formed into bricks.

In connection with the use of extraneous waste carbon materials referredto herein, it is immaterial whether those carbon atoms were everpreviously in any form of coke. Therefore, the examples of the bedsincluding non-coke units such as wood blocks and bricks with carbonmaterial generally intend that the carbon bed have such non-coke unitsin a range of about 25% to 100% and about zero to 75% coke (referring toquantities of carbon atoms in the respective materials), where some ofthat zero to 75% coke may be replaced by carbon of feed materials (otherthan the mentioned non-coke units), up to, e.g., about 10% of the totalcarbon. In some processes it may be favorable to start up a reactor witha bed of coke as has been formerly used. As operation continues afterstart-up, and the coke is consumed, increasing quantities of thenon-coke units can be added.

The carbonaceous beds with the non-coke units of the above examples arebelieved suitable for use in a variety of pyrolytic processes. Just byway of a more particular example, they are suitable for, but not limitedto, use in a PGR process of gasification of biomass or municipal wasteto produce syngas.

The non-coke units are of varied or irregular shape and size to leavevoids in the bed as necessary for gases to flow to carbon reactinglocations and to rise within the bed and exit from the bed. Also, thevoids are for allowing liquids, including molten slag and molten metals,to descend through the bed to an outlet at the bottom.

The mentioned non-coke units are believed superior to coke alternativessuch as anthracite coal or charcoal as significant bed constituents inachieving better properties, closer to those of coke, for efficiency ofreactions while maintaining strength to support working material withoutbeing crushed, which tends to close voids in the bed and impededesirable reactions and flow of molten slag and metals through the bed.Conventional charcoal briquettes, for cooking, are considered relativelyweak in strength compared to coke or the non-coke units presented here.

In addition, the non-carbon components in the coke replacement units(i.e., the mentioned blocks or bricks) can be engineered to be usefuladditions to gasification and/or vitrification processes. Wood, as anexample, typically contains about 35-40% by weight of oxygen, which canreplace a portion of the oxidant being fed to a gasifier as a gas. Also,in vitrification or in gasification processes in which the feed containsinert materials which will exit the process as slag, additives which areneeded to flux or modify the inert materials to produce the desired slagchemistry can be added instead to the brick formula along with thecarbon source. For example, one or more binders in the bricks can beselected to satisfy the requirements of those additives where cementtype binders will typically provide calcium for fluxing properties whilesilicate binders will serve as modifiers to the slag chemistry.

In metal melting applications, where the slag chemistry is an integralpart of the final metal chemistry, the brick formulation can beengineered to incorporate slag making ingredients, resulting in lessneed for a separate feed of those ingredients and to provide moreintimate contact of those materials with the carbon reductant.

In addition to the foregoing, embodiments of the present inventioninclude, either in addition to or independent of the use of thementioned non-coke units, various other ways of constructing oroperating a reactor that can contribute to a lessening of the amount ofcoke required for the carbon bed (as well as consuming some otherwisewaste materials). These include any of the following: using spentpotliner material from the aluminum industry; and/or providing a reactorwith a charge bed (or feed bed) support that is also a gas distributorand a slag screen.

The carbon liner of the potliner is very high in carbon content. It isjoined with refractory material, such as a ceramic. Spent potlinermaterial is a listed hazardous waste that is difficult or expensive todispose of. In embodiments of the present invention, there are a numberof ways to use the material in reactor carbon beds. The carbon can beapplied as particles in the above mentioned bricks (as any other carboncontaining material can) but potliner carbon material may also be usedin particles or chunks that substitute for coke in the bed. Therefractory part of the potliner (sometimes available from aluminummakers intermixed with the carbon liner, or separately) can be placed,in particles or chunks, either in the bricks or otherwise in the bed inaddition to the carbon and be a beneficial slag additive (when used in aquantity that meets the composition requirements for the reactionsoccurring in the bed).

A charge bed (or feed bed) support grid can be disposed horizontallyacross the reactor inner volume below one or more main feed chutes andabove the region in which plasma heated gas is developed. The grid, insome embodiments, has closely spaced grid elements of refractorymaterial with cooling to prolong life, e.g., by inner passages for watercooling in the interior of the grid elements. Operation of the reactoris conducted so that the cooling allows the refractory to survive for auseful period of time but without slots or other grid openings becomingclosed by freezing slag or metal within them. Hot gas flow from theregion below the grid, through the grid openings, will gasify charge bedmaterial on top of the grid and resulting slag from the gasified chargebed material will flow down through the openings. (In this particularexample, very little, if any, of the ungasified charge bed materialwould pass through the small openings of the grid.) This arrangementallows the use of less carbon bed material (coke or otherwise) as wellas embodiments of desirable reactors and their operation with no carbonbed. Furthermore, and more generally, any support for charge bedmaterial above a carbon bed, including a support with openings thatallows some appreciable amount, but not all, of the charge bed materialto fall onto the carbon bed, will still, to some extent, lessen theburden of the charge bed on the carbon bed and, hence, reduce thestrength required for the carbon bed materials to support the chargebed. This, in turn, allows selection from a wider range of carbonmaterial particles or non-coke units, including those that may not havethe strength of coke particles.

A PGR, with innovative feed arrangements configured to enhance a supplyof non-coke feed materials, can be relatively continuous and dependable.An example in this category is the use of an eductor for carbon finesinjection into a carbon bed.

Other reactor configurations can contribute to less consumption ofcarbon in the bed, such as by permitting operation at a lowertemperature. A PGR configured with one or more feed chutes at a heightno greater than just above the top level of a charge bed is a form ofreactor of general utility as well as having a capability to be operatedwith a lower bed temperature if desired. In some instances, reactors areoperated to gasify feed materials that are uncompacted and in piecesthat are diverse in size and weight. (For example, shredded biomass ormunicipal waste including paper products.) A higher percentage of thelight weight feed material pieces can be reacted by hot gases rising upfrom the charge bed where the feed chutes are close to (or under) thecharge bed surface to a greater extent than in prior practice in whichfeed chutes have been located well above the charge bed in an uppersection of the reactor and where more of the lighter pieces of feedmaterial did not descend enough to reach sufficiently hot gases forreaction. A large percentage of the lighter pieces may exit the reactorwith the exhaust gas in that case. In the new arrangement, any lightfeed materials that do not descend directly onto the charge bed are morecertain to float immediately above the charge bed and reach a hightemperature from gases rising from the nearby charge bed so they aregasified. This contributes to the top gas, or syngas, production of thereactor and permits lower demands on the carbon bed, as long as thecarbon bed temperature would still be sufficient to maintain molten slagflow. This arrangement can be applied, for example, and withoutlimitation, where the reactor also has, at about the same elevation asthe charge bed surface and the feed chutes, one or more gas inlets foroxygen (air) that takes part in reactions of the floating feed materialand is regulated to assist in forming carbon monoxide from that feedmaterial.

The carbon beds described in the foregoing examples are generallyapplicable to gasification (or vitrification) reactors with a fixed orstationary bed but are not necessarily limited thereto as they may alsobe applied to fluidized beds. In addition, the carbonaceous beds ofother thermal reactors besides PGRs may be similarly modified to reducecoke requirements.

FIG. 1 is an example of a PGR of general capability for gasification andvitrification of various process materials. One manner of operating sucha PGR is for gasifying material to produce a syngas from the feedmaterial. The feed material may include, as examples, any one or more ofmaterials such as biomass, municipal solid waste (MSW), coal, industrialwaste, medical waste, hazardous waste, tires, and incinerator ash. Thesyngas can contain useful amounts of hydrogen and carbon monoxide forsubsequent use as fuels.

The reactor of FIG. 1, shown in full elevation in its left half andvertically sectioned in its right half, has a reactor vessel 10,generally of refractory-lined steel (the lining is not specificallyshown in the drawing), whose prominent parts include or contain acarbonaceous bed 20 above which is a section for a charge bed 30 ofprocess material, such as biomass, with a freeboard region 40 above thecharge bed 30, and the freeboard region extends up to a roof 50.

The portion of reactor vessel 10 enclosing the carbonaceous bed 20 hasone or more (typically two to four) nozzles 22 (sometimes alternativelyreferred to as ports or tuyeres) for location of a like number of plasmatorches 24 (not shown in detail) for injecting a high temperature plasmaheated gas into the bed 20. The plasma nozzles 22 may additionally bearranged to introduce additional process material that may be desired,such as a gas or liquid (e.g., steam) or some solid particulates, forreactions within the bed 20 along with the material of the charge bed30. (Such additional process material may also be added directly to thebed 20 by nozzles not having a plasma torch.) The reactor vessel 10 alsohas at the bottom a molten slag and molten metal outlet 26.

A part of the reactor vessel 10 that is around the charge bed 30 andabove the carbonaceous bed 20 further includes some additional nozzlesor tuyeres 32 that, usually, do not contain plasma torches but providefor the introduction into the charge bed 30 of further process material,if desired, such as in the form of a gas, liquid, or solid particulates.

The upper feed section or freeboard region 40 of the reactor vessel isarranged with one or more process material feed chutes 42. Here, onefeed chute 42 is shown in a side wall. More generally, one or more feedchutes can be at any location in the side wall of the reactor vessel 10or the roof 50 for depositing feed material initially onto thecarbonaceous bed 20 as well as during operation of the reactor to add tothe charge bed 30 as its process material is diminished by the reactionsthat take place in the reactor.

The roof 50 encloses the top of the reactor vessel 10 except for one ormore outlet ports 52 for gaseous reaction products (e.g., syngas) toexit from the reactor vessel 10. Gas outlet ports may be variouslyprovided either in the roof 50 or the sidewall of the reactor vessel 10.At least where feed material through any feed chutes includesparticulates, it is usually desirable for any gas outlet ports 52 to belocated far enough away from the point of entry of feed material toavoid excessive exiting of unreacted particulate matter through the gasoutlet ports.

The PGR configuration shown in FIG. 1 is generally in accordance with anexample embodiment of the copending application of Dighe et al., Ser.No. 12/378,166, filed Feb. 11, 2009, Patent Application Publication No.2010/0199557, Aug. 12, 2010, which, among other things, includes agenerally upwardly and continuously expanding conical wall 12 of thereactor vessel 10 which can provide beneficial gas flow characteristicsin the charge bed 30 and the freeboard region 40. Said application isincorporated herein by reference for its description of reactorconfigurations, including variations of that shown in FIG. 1, and theiroperation. The present invention, however, is not restricted to reactorswith such configurations.

PGR practice, and practice with other types of pyrolytic reactors with acarbonaceous bed, has used, at least almost always, a bed that issubstantially all of coke. Coal is sometimes mixed with the coke but anyother carbon bearing material has been very minor and incidental to thestructure and operation of the reactor. Coke has a composition with ahigh content of carbon (about 90% by weight), it can be formed invarious shapes and sizes so particles of coke, e.g., with averagecross-sectional dimensions of about 10-15 cm., can have ample carbonsurfaces for reactions, provide voids for upward gas flow and downwardflow of liquids, and strength sufficient to maintain voids throughoutoperation. The full size distribution or variation of particles of acarbon bed with coke is preferred to be greater than about 5 cm. toprevent the void spaces from being too small for proper liquid flow andless than about 25 cm. to minimize material handling issues. Where up toabout 10% of the carbon in the bed 20 is of finer carbon particles (e.g.injected directly into the bed 20), adequate voids for liquid flow canbe maintained.

In the PGR of FIG. 1, the carbonaceous bed 20 (hereinafter sometimesreferred to as a C bed) includes non-coke material to a significantextent, during at least some of its operation, such as at least about25% of the C atoms of the bed being not in coke units. For that reason,in FIG. 1, the carbonaceous bed 20 is further identified by the legend“C BED WITH NON-COKE”.

Examples of non-coke materials for use as at least part of the bed 20are natural wood blocks and, also, bricks including particles of acarbon-bearing material with one or more binders. The non-coke materialsare formed in particles or units of irregular size and shape so thatwhen placed or assembled in a bed they have exposed surfaces resultingfrom voids that occur between some parts of them. The non-coke units ofthe bed 20 are generally of the same size range as the coke particlesfor reactor beds as discussed above, but are not limited thereto.

An initial carbonaceous bed 20 of a PGR, such as that of FIG. 1 isgenerally established in the bottom of a reactor vessel 10 prior tooperation of the reactor with feed material or powered up plasmatorches. Then, once an initial bed 20 is in place, operating with activeplasma torches 24 and depositing feed material to form a charge bed 30commences. Most such processes are substantially continuous over aperiod of at least many hours with additional feed material applied,perhaps continuously or at least in frequent intermittent quantities.The reaction of the plasma heated gas with the C bed 20 inherentlydepletes carbon from the C bed. However, the rate at which the carbon inthe bottom carbon bed 20 is consumed is much lower than the rate atwhich the feed material is gasified. Therefore, an initial C bed 20 onlyrequires minor additions of carbon material in the course of processinga much larger amount of feed material. Some aspects of adding carbonmaterial to an initial C bed are described below.

Typical operations, such as for production of a syngas, include forminga charge bed 30 on top of the C bed 20 by depositing feedstock throughthe feed chutes 42 where the feedstock may be, for example, biomass,municipal waste, coal, or mixtures thereof. During or after formation ofan initial charge bed 30 that extends above the additional nozzles 32,those nozzles are used to inject fluids such as air, oxygen, or steaminto the charge bed 30 while the plasma torches 24 operate with a torchgas, such as air, and, perhaps some steam or other fluid or smallparticles of solids are injected into the C bed 20 through the nozzles22.

For production of syngas, to exit through the exit ports 52, it isdesirable to operate in a manner to produce carbon monoxide andhydrogen. Carbon dioxide may be produced to some extent but carbonmonoxide can be favored under conditions that limit air or oxygen inrelation to carbon in the reactor.

As mentioned above, in such an operation, the reactor will consumecarbon of the C bed 20 and the carbon is desirably replenished so thequantity of carbon is not appreciably reduced. A way of doing that inthe past, for a coke bed, has been to add coke to a feedstock charge bedon top of the coke bed. For example, in production of syngas frombiomass material, there has been coke added along with, i.e., mixed withor in alternate batches with, biomass. Processes have been performed inwhich such added coke amounts to about 5% by weight of the total offeedstock including coke.

Such carbon replenishment is also a consideration where the C bed 20 isto include non-coke material as described. Consequently, in accordancewith one embodiment, the carbon material supplied to replenish the C bed20 can be similar to the nature of an original C bed with non-coke andinclude at least about 25% of the added carbon being from non-cokematerials. In some instances, for example, because of lower carboncontent (compared to coke) of non-coke units that may be used, it wouldbe desirable to make the total material of the C bed a greater quantitythan in prior operation with just coke so there is an equivalent amountof carbon atoms in the bed.

The C bed improvements described herein, such as the use of wood blocksor carbon containing bricks as some or all of the bed (in lieu of coke),can also be applied to C beds in reactors without plasma torches. Insuch reactors, a C bed may be initially activated by ignition of a fuel,such as natural gas, supplied for a brief time as formerly practicedwith a 100% coke bed of such a reactor.

FIG. 2 shows an enlarged view of just a part of the apparatus of FIG. 1.The C bed 20 of FIG. 1 is shown in some additional detail to showindividual particles 21 within the bed 20 and voids 23 occurring withinthe mass of the particles 21 due to the mixed size and irregularconfigurations of the particles. The size and shape of the particles 21can vary widely. Just for example, the particles 21 may have an averageof their dimensions in a range of from about 5 cm to about 25 cm, ofwhich about 10 cm to 15 cm is an example of the average size of cokeparticles and about 10 cm to 25 cm for the average size of non-cokeparticles.

FIG. 3 shows an additional enlarged portion of a C bed 120 withparticles 121 and voids 123 where the particles 121 are natural woodblocks.

The natural wood blocks or particles 121 are, for example, waste from aprior industrial source process such as the manufacture of wood palletsor are formed especially for use in the C bed 120. It is generallyunnecessary to dry or treat the wood block particles (such as bycharring any surface portions of them before applying them to the bed120), although either or both some drying and charring can be performedif desired before placement in the bed 120. The wood block particles 121can be added to a bed 120 that includes coke particles with or withoutintermixing the materials to produce any particular degree ofhomogeneity.

The wood for the wood blocks 121 can be of various plants or trees.Hardwoods such as oaks are one suitable wood material. Such woods, andthe wood blocks 121, have a typical carbon content of about 50% byweight.

FIG. 4 shows an additional enlarged portion of a C bed 220 withparticles 221 and void 223 where the particles 221 are bricks formed ofcarbon containing particulate material (e.g., wood chips, carbon fines,or a mixture of carbon containing material particulates). The bricks 221may sometimes be referred to as “briquettes” but are distinct fromcommon charcoal briquettes as explained further below

FIGS. 2-4 are primarily to give just a rough idea of the appearance ofthe particles and voids referred to. The respective C beds 20, 120, and220 need not always fully occupy the bottom portion of a reactor.Normally, any of the carbon beds discussed in a plasma reactor wouldextend up at least past the location of plasma torches, such as one thatmay be located in a plasma nozzle 222 of FIG. 4.

The bricks 221 of FIG. 4 can be molded, without any applied pressure orheat being necessary, of a mixture of the carbon particulates with oneor more binders. Portland cement is one suitable binder. Otherconstituents may be included, for example as binders, or as fluxants orglass formers, and/or as catalysts. Some examples of bricks 221 havebeen formed of a mixture that included, by approximate weight percent,40 parts carbon fines, 8 parts Portland cement, 4 parts bentonite clay,4 parts sand (SiO₂), 12 parts sodium silicate, and 32 parts water. Suchbricks have been made with a carbon content of about 66% by weight on adry basis.

Other bricks 221 have been formed of a mixture that included, inapproximate weight percent, 23 parts carbon fines, 21 parts Portlandcement, 11 parts sand, and the balance (45 parts) water.

The bricks 221 can be molded to any size (similar in general size tocoke particles) and shape, with characteristics to provide desirablevoids in the bulk bed. It is not a necessity to vary the size or shapeof bricks formed for use as bed particles such as the particles 221 ofFIG. 4. It can be suitable, as well as economical, to use a single moldsize and shape if desired. Same sized cylindrical (or spherical) unitswill inherently provide voids in the bed. Multiple-sized units can alsobe made and used together, if desired, preferably with a cross-sectionalsize distribution of about 5-25 cm. for most all the units and only aminor amount of any smaller carbon bearing units that tend to reducevoids.

Pressure and/or heat are also suitable means to form bricks withsufficient strength with a low quantity of, or no, binding agents.Generally speaking, and without limitation, examples of bricks formedwith a cement binder are favored where the strength of the bricks isimportant.

The carbon particulates in the bricks 221 can be “carryover” particlesfrom a gasification reactor and in this way provide a means of recyclingcarbon otherwise lost to the process resulting in increased carbonutilization and therefore higher efficiency. Carryover particles areunreacted or partially reacted particles that exit a reactor with gasesfrom the reactor. They are generally desirable to be minimized but somewill almost certainly result from any gasification process. Thecarryover particles can be made use of as part of the non-coke contentof a C bed in bricks or introduced into a reactor as part of the feedmaterial (at chutes such as 42, FIG. 1) or otherwise (e.g., throughplasma nozzles 24 or nozzles 32 of FIG. 1).

In general, the carbon particulates (or “fines”) used in making thebricks 221 are particles having average cross-sectional dimensions in arange of from about one micron to one centimeter and collectively have atotal weight percent of carbon of at least about 50%. The average sizerange mentioned is not to exclude particles outside that range;particles finer than one micron can be quite suitable.

Combustion processes including boilers and incinerators also generatecarryover particles such as fly ash and these materials may containuseful quantities of carbon that may serve as a source of carbon forcarbon bed bricks. In addition, the properties of fly ash are alsoadvantageous to the brick forming process allowing a reduction in theamount of calcium based cement binders that is needed.

The addition of materials to the bricks 221 which behave as catalysts,such as, but not limited to, nickel or iron, is another advantage of thebricks over coke alone as the carbon bed material. In this manner, thebrick can be engineered to provide not only a functional source ofcarbon to the plasma gasification process and the fluxing agents neededto properly vitrify the inert materials contained in the feed beinggasified, but also catalysts to cause certain desirable chemicalreactions to occur.

One example of a catalyst inclusion in the bricks 221 is an addition ofnickel or iron to the bricks on the order of a few percent by weight tocatalyze the C+NO reaction to reduce the NO in the syngas to N₂+O₂. Thisis especially important in bioreactors converting syngas to liquidfuels. Formerly such catalysts, when used to minimize NO_(x), had to beadded with the feed material to the charge bed.

The following table gives additional examples of formulations fornon-coke bricks, such as the bricks 221 of FIG. 4.

TABLE I Constituent Range (wt %) Formula A Formula B Formula C Formula DFormula E Formula F Carbon 40-95  65  70 60 41 45 80 Silica 0-30 6.57-14 10 19 15 Calcium Carbonate 0-25 Fly Ash 0-40 10 20 Portland Cement0-20 13 39 20 Potassium Silicate Cement 0-20 8-14 20 Aluminum SilicateCement 0-20 5 Kaolin Clay 0-20 Sodium Bentonite 0-20 Calcium Bentonite0-20 5.5 5-6  15 Potassium Bentonite 0-20 Sodium Silicate 0-20 10Aluminum Hydroxide 0-10 2-3  Nickel 0-5  Iron 0-5  1 100 100 100 100 100100The amounts, and ranges of amounts, are all in approximate weightpercent of the overall composition that is mixed with water added (atleast sufficient for cement hydration). The carbon is of particulates orfines as previously described. Binders include the cements and the clayor bentonite materials listed. Silica is a glassifier. Calcium carbonate(lime) is a flux agent. Fly ash also has fluxing properties; it alsocontributes some additional carbon to the mixture (typical fly ash isabout 5% carbon). Sodium silicate (or water glass) is also a glassifier.Aluminum hydroxide contributes to binding. The additional constituentsmentioned are nickel and iron which serve, if used, to help avoid NO_(x)emissions as was previously discussed.

The initial column of ranges (before columns with Formulas A through F)shows an upper limit of about 95 wt. % for carbon particles, and aminimum of 0 wt. % for all the other constituents listed. Thatindicates, in any specific formulation, each of the secondaryingredients is individually optional but at least about 5 wt. % of oneor more of them (e.g., binders) would be included with the carbonparticles. Also, it is to be understood that Formulas A-F are mereexamples without exclusion of others consistent with the ranges given inthe first column. Therefore, for example, other formulations may includesome amount of calcium carbonate, kaolin clay, sodium bentonite,potassium bentonite, and/or nickel even though Formulas A-F include noneof those constituents.

An example process for forming bricks is for the ingredients of aformulation, such as Formula A, to be dry mixed followed by the additionof water at a weight ratio about one part water to two parts dry mix.The mixture is placed in molds of the desired size and shape and allowedto set up and air dry.

Some examples have been made in molds that produce short cylinders ofvaried sizes. The particles 221 of FIG. 4 represent such cylindricalunits, where the rectangular appearing units are, or can be, cylindersviewed from the side.

A further example of processing is for the constituents of aformulation, such as Formula F of the Table, which has a relatively highC content, to be dry mixed followed by pressing the mixture into moldsunder pressure sufficient to solidify the bricks to the desired shapeand size and then placed or fed into a reactor in a “green” state. Theoperating temperature of the reactor quickly cures the bricks to theirfinal composition.

Any known brick making techniques may be applied for making the non-cokebricks such as the bricks 221 and the compositions are to generallyinclude carbon particles in one or more binders adequate to make strongunits along with optional quantities of flux agents, glassifiers, andcatalysts like, or similar to, such additives to prior reactor carbonbeds with coke.

“Carbon particles” referred to as brick constituents need not be 100% Catoms but the nature of the particles can influence how much particlematerial to use. Wood chips have adequate carbon for use in bricks butmost likely in a greater quantity than carryover C particles.

An additional set of formulations for bricks can replace purer Cparticulates with wood particles that can vary in size from fine sawdustto wood chips. In such formulations, the total composition may have upto about 95 parts (weight %) of the wood with lesser amounts of theother constituents mentioned in the Table above, in addition to thewood. By way of further example, a particular composition of that typeincludes 5 parts silica, 15 parts Portland cement, 5 parts calciumbentonite, and 75 parts of the wood. All would be mixed, perhaps withwater, and molded or pressed as described above. In general, therelative amount of binder (and selection of a particular binder) will bedetermined by the size of the wood particles with the objective toenhance the quantity of wood, and hence carbon, in the bricks. Wood, andother biomass, particles generally have some volatilizable constituentsthat are driven off as a brick with such particles is heated. That isfavorable for brick porosity.

Clearly, other formulations may include both wood particles as well asother carbon particles in non-coke units, they can be fed to the chargebed 30 through a feed chute, such as the feed chute 42 of FIG. 1 or someother, just as coke has been in the past, and they will (at least almostentirely) remain unconsumed as they descend through the charge bed 30 tothe C bed 20.

Any of the shapes of particle units 21, 121, or 221 shown in FIGS. 2, 3,and 4 are just some suitable examples for non-coke units that can beapplied.

By way of further clarification of examples, any of the compositionspreviously mentioned, such as in the discussion of Table I, may bevaried to include wood (or other biomass) particles, or other carboncontaining items with other elements, in place of some or all of thepurer carbon particles (e.g., coal fines) in which case the compositionwould be adjusted to have a similar net amount of carbon atoms. To theextent wood or other biomass is used instead of coke or other mineralsources for the carbon content, there is a corresponding avoidance offossil fuel use.

An example composition of the use of wood particles as the source ofcarbon in bricks is one with (in approximate weight % excluding water tobe added), 75% wood particles, 5% silica, 15% Portland cement, and 5%calcium bentonite; in this case without any carbon from a fossil source.The wood particles may be, e.g., sawdust, wood chips, or a mixturethereof. The binder contents could be varied to maximize the amount ofwood, and hence carbon, in the bricks consistent with adequate bindingof the wood particles that are used.

Another favorable aspect is the facility in which the C bed compositioncan be varied over a course of operation. For example, one could electto start up a reactor with a C bed of a high carbon source, such ascoke, to limit the initial slag formation. This may be the case if the Cbed is used to initially heat up the vessel and before it is hot enoughto melt more inert material. Then, as heat-up is continued andcompleted, bricks, such as described above, can be introduced withresulting greater slag formation.

Some example bricks that have been made according to the foregoingdescription and used in place of some of the coke in a PGR gasifyingbiomass (and forming slag tapped from the reactor) with satisfactoryperformance substantially matching that of an all coke bed have includedthe following compositions of Table II.

TABLE II #1 #2 #3 Dry weight % Dry weight % Dry weight % Coal Fines 68.677.1% 0.00% Lime (CaCO₃) 13.7% 16.7% 9.12% Sand 11.8% 0.0% 10.94% Cement(Portland) 5.9% 6.2% 32.76% Char 0.0% 0.0% 47.18%

Table II gives the weight percentage of the dry ingredients. Water addedand mixed with the dry ingredients was, in the case of batch #1, about10% of the dry mix weight, and for batch #2, about 20% of the dry mixweight, and for batch #3, about 15% of the dry weight mix.

In general, the brick compositions referred to are for the startingmaterials and the resulting compositions of finished bricks is notsignificantly different other than the absence of water.

One of the favorable aspects of the use of bricks in accordance with theinvention, over the use of coke, is the ability to vary the compositionof the bricks. That can be done for reasons including the nature andcomposition of the feed material into the reactor. The examplecompositions of Table II were particularly chosen for use with biomassfeed material.

Without limiting the above description, the following additionalexamples of making and testing non-coke brick units are provided.

The starting materials include, in approximate dry weight %,

Coal fines (averaging less than 5 mm. size) 60% Lime (CaCO₃) 20% Sand10% Portland Cement 10% 100%

Weighted amounts of the dry ingredients (with a total weight of 100 to300 kg.) are dry mixed in a cement mixer about 5 to 10 minutes andbecome thoroughly intermixed. Water is slowly added to the mixer so asto have the water incorporate with the dry ingredients and the mixtureto have wetness only to extent it can set, and not any wetter. (It isfound that excess water may result in bricks with a higher density, andmore limited porosity, than is generally desirable.) After sufficientwater is added, mixing is continued about 5 minutes longer to insure themixture's readiness. (Water makes up about 15-25% of the total mixedmass.)

Molds are made of about 12 cm. lengths of PVC pipe having an innerdiameter of about 10 cm. The mixture is placed in the molds and allowedto set about 3 to 5 minutes before the molds are removed by lifting themfrom around the bricks that have set.

The bricks are then allowed to air dry and cure for about 72 hours. Asample of the bricks can be subjected to a drop test as a strengthassessment. The drop test may be to drop the bricks from about 3 metersonto a hard (e.g., concrete) surface and observe whether the brickscrumble (i.e., break into any more than about 2-3 large pieces). If theycrumble, that suggests they require more drying or the composition wouldbe better changed by increasing the cement amount by an additional 1-2%of the dry weights.

Once satisfactorily strong bricks are formed, they may be used in areactor immediately or later, if kept reasonably dry.

A comparison test can be performed in which successive phases ofoperation are conducted in a reactor including:

Phase O-Baseline; C bed of coke; 1-3 days operation;

Phase I; 25% carbon addition of bricks; 12 hours;

Phase II; 50% C from bricks; 12 hours;

Phase III; 75% C from bricks; 12 hours;

Phase IV; 100% C from bricks; 12-24 hours; and

Phase V; return to 100% C from coke; 24 hours.

During each phase there is monitoring of all significant parametersincluding: temperatures and pressures at several levels in the reactor;data on feed rates; amounts and rates of slag production; syngas volumeand its O₂ and CO level; and plasma torch conditions, including torchpower, amperage, voltage and air, including torch air, shroud air, andspare nozzle air.

All of the above, and similar tests with other brick compositions,confirm that bricks are capable of replacing significant amounts of cokewith satisfactory overall reactor performance.

As mentioned before, carbon particles incorporated into bricks, such asthe bricks 221, can come from any carbon particle source. Some sourcesare made extra attractive because they allow economical use of carbon inmixtures or forms that is otherwise difficult or expensive to disposeof.

The earlier discussion mentioned the use of spent potliner-carbonmaterial from the aluminum industry. In normal aluminum making, suchmaterial is contaminated with cyanide (CN). It is often available totake from a manufacturer for no cost, or with a payment to the partytaking it. Furthermore, the potliner carbon can be used either, or both,as particles in bricks or as chunks, like particles 21 of FIG. 2, as Cbed material without processing into bricks. Additionally, therefractory (ceramic) material is also available for use in the bricks,or directly in a bed, to serve as a flux.

Spent potliner (or SPL) material is known that in the total compositionof carbon and refractory material includes about 23% pure carbon. Otherconstituents include quantities of metal oxides, e.g., SiO₂, Al₂O₃, andNa₂O which may also be useful in a gasifier to some extent.

The SPL, as made available by aluminum manufacturers, may be separatedinto what is called a “first cut” that includes about 55 to 65% C andless of the metal oxides. This is the hazardous material needed to bedisposed of under government regulations. When so separated, there is a“second cut” of nonhazardous material that includes more of therefractory material of the potliner and has only about 1 to 5% C and amore significant amount of metal oxides, all of which can be made useof, in some quantities and relative amounts, in the gasifiers that relyon a carbon bed and fluxing and glassifying agents to help fluids flowthrough the bed.

Another source of otherwise unwanted carbon waste that is usable in thenon-coke bricks is from soot water produced by gasifiers. A number ofcurrently operating gasifiers (e.g., for gasifying coal, heavy oils,etc.) produce a usable and desirable syngas but also create a soot waterbyproduct which has to be disposed of. As used here, the “soot water”may include any ungasified fuel constituents as well as metals and slagelements that may accompany the ungasified fuel.

FIG. 5 shows a block diagram of one example of dealing with such sootwater. In this example, the soot water resulting from some other(“conventional”) gasification (block 510) is subjected to filtrationwith water being removed (block 512) and some filtered carbon beingrecycled back to the prior gasifier (feedback line 514). The remainingsolids are formed into a filter cake (from the filtration 512) thatpreviously had to be disposed of, such as in a landfill, but is nowinstead fed into a PGR (block 514) to yield additional raw gas (syngas)516 and slag and metals 518 (that may have economic value).

By the present invention, soot water residue, such as a filter cakeresulting from soot water filtration may be applied as C particleswithin bricks (like bricks 221 of FIG. 4) as well as being introduced inother ways into a PGR). (Filter cakes may be formed or ground down toyield suitably sized C particles).

As mentioned before, carbon bearing particles of a wide variety may beused in the bricks to be used as non-coke units in a C bed. Additionalto the other mentioned sources are plastic materials. Plastic objects(e.g., waste plastic containers) may be mechanically reduced (e.g., byshredding) to form particles for inclusion in the bricks. Some commonplastics that may be used instead of or mixed with, other C particlesfrom sources such as coal or biomass are the following and theircomposition:

TABLE III HDPE PET PVC LDPE Carbon 84.38% 62.28% 45.04% 67.13% Hydrogen14.14% 4.14% 5.60% 9.70% Oxygen 0.00% 32.88% 1.56% 15.80% Nitrogen 0.06%0.00% 0.08% 0.46% Chlorine 0.00% 0.00% 45.32% 0.00% Sulfur 0.03% 0.00%0.14% 0.07% Ash 1.19% 0.50% 2.06% 6.64% Water 0.20% 0.20% 0.20% 0.20%TOTAL 100.00% 100.00% 100.00% 100.00%

When such materials are used, for example in brick formulations such asthose of Table I, the quantity may be adjusted to provide the desiredamount of carbon. Because of the volatile constituents of the plastics,they, like biomass particles, devolatize and provide added porosity whenheated.

Heating of bricks (whatever the C source) may be performed either priorto use in a gasifier or in a gasifier in operation. The latter, in-situreacting of binder elements and driving off volatiles, saves on energycosts.

FIG. 6 illustrates one example of a PGR with a grid or distributor plate600 as was generally disclosed in the earlier discussion. Only a lowerportion 610 of a PGR is shown with a thermal bed region 620 and a chargebed region 630. The plate 600 serves as a support for the feed bed 630,as a gas distributor for gas heated in the thermal bed region 620 and asa slag screen for descending molten material. For these multiplepurposes, the plate 600 has a screen-like structure with grid elements601 of refractory material and openings 602 (for gas and liquid flow).The screen or plate 600 of refractory material is equipped with acooling arrangement, such as inner passages 604 for cooling water. Theopenings 602, in this example, are intentionally quite small, e.g., nogreater than about 10 mm, to limit or exclude charge material from thebed 630 from falling through to the lower region 620. But the openings602 are large enough, e.g., at least about 3 mm., to allow easy flow ofgases (e.g., oxidant heated by a plasma torch in a nozzle 622 fromregion 620) up into the charge bed 630 and easy flow downward of moltenslag and metal through the screen 600 into region 620 for exitingthrough an outlet port 626 at the bottom of region 620.

Region 620 may contain a carbon bed. If it does contain a carbon bed, itmay be of lesser extent than in usual PGR beds and may include any typeof carbon material without concern for whether the material is strongenough to support the charge bed without collapsing and eliminating thevoids that enable gas and liquid flow. Here the charge bed 630 issubstantially supported on the plate 600.

In alternate embodiments in which a grid or plate is used with largeropenings allowing some solid charge material to pass down to a C bed ina lower region, such a grid or plate may still allow some greaterflexibility in the selection of carbon bed material because of at leastpartial support by the grid.

A PGR 610 of FIG. 6, and more generally any PGR with a plasma heated gasregion 620 at a level from which hot gases rise into a process material,can be operated with little or no carbon bed and still achievegasification of process material. The arrangement of FIG. 6, with thedistributor plate or grid 600, can be favorable for operating without aC bed because the gas and liquid flows are not dependent on voidsoccurring in either in a C bed or within process material. This form ofoperation, whether with the PGR of FIG. 6 or some other, such as that ofFIG. 1 but without the C bed, means the plasma heated gas input to thelower region provides all the energy for reactions, rather than gettinga major contribution of thermal energy from a heated C bed, and alsomeans carbon atoms for forming desirable product gas, such as a CO, areall from feed material in the absence of a C bed. Any such mode ofoperation can, of course, completely avoid any need for use of coke inthe reactor.

FIGS. 7A and 7B show elevation and plan views of a PGR reactor 700 thathas general utility and, furthermore, can be operated in a manner thatis favorable in some respects to overall efficiency of thoroughreactions of process material with less dependence on energy from a Cbed.

The reactor 700 is similar to that of FIG. 1 in several respects butwith certain differences. A reactor vessel 710 is provided with a carbonbed region 720 above which is a charge bed region 730 and a freeboardregion 740 up to a roof 750 with gas exit port 752. In this example, thewall of the reactor vessel 710 has a cylindrical portion that enclosesthe C bed region 720, a first conical portion with upward expansion thatencloses the charge bed region 730 and also a region 735 just above thecharge bed in region 730 (the top of which is represented by the line731 in FIG. 7A). The wall of the reactor vessel 710 has a second conicalportion with upward expansion enclosing the freeboard region 740. Theconical portion for region 740, in this example, is at a lesser angle tothe center axis of the reactor vessel 710 than that for the regions 730and 735, an aspect that can contribute to beneficial gas flow in thoseregions.

In the example reactor 700 there are one or more plasma torch nozzles722 to the carbon bed region 720, and there are additional nozzles ortuyeres 732 to the charge bed region 730, which may all be like orsimilar to such features of FIG. 1. There is also a molten slag andmetal outlet port 726 from the C bed region 720. However, in reactor700, there are one or more (three are shown) feed chutes 736 into theabove-charge bed region 735 rather than well above as the feed chute 42is shown in FIG. 1. (The lower feed chutes 736 are considered normallysufficient to replace any higher feed chutes but do not necessarilyexclude provision of one or more additional feed chutes anywhere in thereactor wall or the roof 750 to region 740.)

The feed chutes 736 to the above-charge bed region 735 each havematerial feeding mechanisms 737 exterior of the reactor 700 forsupplying feed material through the chutes 736. It is generallypreferred, such as for economical operation, that the mechanisms 737 besuch as to allow feed material to be supplied into the reactor 700substantially continuously, at a fairly uniform rate, and that it can besupplied without need for extra steps to compact the feed material intomore solid blocks of material. Loose biomass or municipal waste, forexample, can be so processed. One example for the feed mechanism 737 isa screw feeder of which there are commercially available units availablefor moving materials.

By way of further example, a reactor 700 as shown in FIGS. 7A and 7B canbe (in exterior dimensions) about 20 to 30 m. in total height with acylindrical bottom portion for C bed region 720 about 3 to 5 m. high, acharge bed region 730 having a wall at an angle to the axis of about10-15°; extending up from the C bed region 720 by about 4 to 6 m., andthe above-charge bed region 735 extends approximately 2 to 3 m. abovethat with a wall angle the same as for region 730 in which the openingsof the feed chutes 737 occur with a vertical dimension of about 0.5 to1.5 m. The vertical heights given for regions 730 and 735 may overlap tosome extent depending on charge bed conditions. Together they can beexpected, in this example to total about 8 to 12 m. for the totalvertical height of the first conical wall portion between levels 738 and739. The height of the region 740, at a wall angle of about 5-10° (orabout 3-6° less than the angle of the charge bed region 730), can be inthe range of about 8 to 12 m. above the region 735. In this example, andgenerally for PGRs with similarly low feed chutes, it is the case thatthe feed chutes are located no more than about halfway up from the verybottom of the reactor vessel and/or no more than about 1 m. above thenormal height of the charge bed in the reactor.

As a consequence of the location of the feed chutes 737, it is the casethat pieces of light weight feed material, such as small pieces ofbiomass and paper pieces of municipal waste material, that tend to floatabove the charge bed due to upward gas flow, have a greater chance ofreaction with the hot gases. In contrast, reactors with feed chutes suchas that shown in FIG. 1, when operated with the same kind of feedmaterial, can have a greater proportion of lighter pieces blown out ofthe reactor through the exhaust ports or float in the reactor at a highlevel at which the rising gases have cooled to an extent that thereaction efficiency is low.

While a reactor such as that of FIGS. 7A and 7B can be operated with acarbon bed of coke or any of the non-coke units described herein and thecarbon bed will include about the same quantity of carbon atoms asformerly, it also happens that the extent to which hot gas energypromotes reactions of these lighter particles and pieces of feedmaterial and contributes to the output of syngas, there can be somewhatlower demands on (less consumption of) carbon in the carbon bed andresulting overall less use of the carbon, whether as coke or non-coke.

An additional aspect of the reactor 700 of FIG. 7B is that within theabove-charge bed region 735 there are one or more gas inlets 734 to theregion 735. In addition to any air or other gases allowed to enter thereactor through the feed chutes 736 (typically not preferred to be alarge amount), the gas inlets 738 can be used for controlled quantitiesof gas, such as air or oxygen, to further promote the reactions of thelighter materials that float in the region 735. It is essentially alwaysthe case, where the objective is to produce a useful syngas, to operateunder controlled conditions of relative amounts of carbon and oxygen topromote oxidation of carbon to produce carbon monoxide (CO) rather thancarbon dioxide (CO₂).

Feeding material to a charge bed, such as in region 730 of FIG. 7A, mayalternatively or additionally be performed in a manner that may bereferred to as “underfeeding”. In that case, a feed chute (i.e., any oneor more such chute), such as one previously described or other feedingdevice, would be located to be capable of delivering the feed materialat a level below the level of the normally occurring top of the feed bedwhile still above the C bed of the reactor. Example embodiments of suchan arrangement include those in which a feed chute like or similar tothe feed chute 736 of FIG. 7A in form, but not in location, is locatedwith its opening into the reactor 700 below the level of the line 731 inFIG. 7A. In this way, the processing of fine particles or light densitymatter in the feed material fed to the feed bed can be even morecomplete, to the extent that substantially all of the feed material iscompletely processed and essentially none goes out of the reactor withthe gas output.

FIG. 8 illustrates an innovative arrangement for introducing carbon intoa gasifier reactor 800, which may be a PGR as previously discussed oranother form of gasifier with a C bed 820. The system includes a supplyof carbon fines 801, here shown as a mixture of sand and coal fines,that is gravity fed through a device such as a rotary airlock 802 tolimit air entry. The solids from the airlock 802 descend to a junction803 at which a top gas recycle loop 804 feeds in some fraction of gasgenerated in the gasifier 800. The solids, with the top gas, are carriedtogether in a conduit 804 to an eductor 805 (a known type of device fordrawing a low pressure gas, such as the top gas, to apply it to a higherpressurized region). The eductor 805 is fed pressurized gas, preferablyan inert gas such as nitrogen, 806 whose flow draws in the top gasstream and solids so that the combination 807 is pressurized enough toenter the gasifier C bed 820. This allows controlled input of carbonparticulates, such as coal fines, and additional flux or glassifieragents, such as sand, into the C bed 820 (through any nozzle opening,with or without a plasma torch). This can result in efficient use ofsuch fines and supplement the carbon of the carbon bed to a degree thathelps lessen need for other carbon such as coke.

Consequently there is seen to be a variety of ways for utilizingnon-coke, and non-fossil fuel, units in carbonaceous beds of plasmagasification reactors and other similar reactors. The foregoingdescription provides a number of examples, but not necessarily all formsand variations of ways for practicing the invention.

What is claimed is:
 1. An apparatus comprising: a reactor vesselcontaining a carbonaceous bed and having means for establishing anelevated temperature within the carbonaceous bed; and the reactor vesselalso having one or more feed material inlets above the carbonaceous bedfor depositing process material from outside the vessel onto thecarbonaceous bed, one or more gas exhaust ports above the bed for exitof gaseous products from the vessel, and one or more slag ports at thebottom of the carbonaceous bed for exit of molten and vitreous materialfrom the vessel; wherein the carbonaceous bed comprises bricks thatcontain carbon and are of varied size and shape of which at least 25% ofthe total carbon content of the bed comprises spent pot liner materialfrom aluminum processing, and wherein the bricks further comprise atleast one of: Portland cement, potassium silicate cement, or aluminumsilicate cement.
 2. The apparatus of claim 1, wherein the bricks furthercomprise soot water residue from a gasification reactor.
 3. Theapparatus of claim 1, wherein the carbonaceous bed includes at leastabout 50% of the carbon content being non-coke units and up to about 50%of the carbon content being coke.
 4. The apparatus of claim 1, whereinthe bricks further comprise one or more of: bentonite clay, sand, sodiumsilicate, and aluminum hydroxide.
 5. The apparatus of claim 1, whereinthe bricks comprise: between 40% and 60% of the spent pot liner materialby weight.
 6. The process of claim 1, wherein the bricks have a materialcomposition including, in approximate weight % other than water: carboncontaining particles, 40 to 95 parts, silica, 0 to 30 parts, calciumcarbonate, 0 to 25 parts, fly ash 0 to 40 parts, Portland cement, 0 to20 parts, potassium silicate cement, 0 to 20 parts, aluminum silicatecement, 0 to 20 parts, kaolin clay, 0 to 20 parts, sodium bentonite, 0to 20 parts, calcium bentonite, 0 to 20 parts, potassium bentonite, 0 to20 parts, sodium silicate, 0 to 20 parts aluminum hydroxide, 0 to 10parts, nickel, 0 to 5 parts, and iron, 0 to 5 parts.
 7. The apparatus ofclaim 1, further comprising: additional inlets through the side wall ofthe reactor vessel for injection of carbon fines into the carbonaceousbed.
 8. An apparatus comprising: a reactor vessel containing acarbonaceous bed and having means for establishing an elevatedtemperature within the carbonaceous bed; and the reactor vessel alsohaving one or more feed material inlets above the carbonaceous bed fordepositing process material from outside the vessel onto thecarbonaceous bed, one or more gas exhaust ports above the bed for exitof gaseous products from the vessel, and one or more slag ports at thebottom of the carbonaceous bed for exit of molten and vitreous materialfrom the vessel; wherein the carbonaceous bed comprises bricks thatcontain carbon and are of varied size and shape of which at least 25% ofthe total carbon content of the bed comprises soot water residue from agasification reactor, and wherein the bricks further comprise at leastone of: Portland cement, potassium silicate cement, or aluminum silicatecement.
 9. The apparatus of claim 8, wherein the carbonaceous bedincludes at least about 50% of the carbon content being non-coke unitsand up to about 50% of the carbon content being coke.
 10. The apparatusof claim 8, wherein the bricks further comprise one or more of:bentonite clay, sand, sodium silicate, and aluminum hydroxide.
 11. Theapparatus of claim 8, wherein the bricks comprise: between 40% and 60%of the soot water residue by weight.
 12. The process of claim 8, whereinthe bricks have a material composition including, in approximate weight% other than water: carbon containing particles, 40 to 95 parts, silica,0 to 30 parts, calcium carbonate, 0 to 25 parts, fly ash 0 to 40 parts,Portland cement, 0 to 20 parts, potassium silicate cement, 0 to 20parts, aluminum silicate cement, 0 to 20 parts, kaolin clay, 0 to 20parts, sodium bentonite, 0 to 20 parts, calcium bentonite, 0 to 20parts, potassium bentonite, 0 to 20 parts, sodium silicate, 0 to 20parts aluminum hydroxide, 0 to 10 parts, nickel, 0 to 5 parts, and iron,0 to 5 parts.
 13. The apparatus of claim 8, further comprising:additional inlets through the side wall of the reactor vessel forinjection of carbon fines into the carbonaceous bed.
 14. An apparatuscomprising: a reactor vessel containing a carbonaceous bed and havingmeans for establishing an elevated temperature within the carbonaceousbed; the reactor vessel also having one or more feed material inletsabove the carbonaceous bed for depositing process material from outsidethe vessel onto the carbonaceous bed, one or more gas exhaust portsabove the bed for exit of gaseous products from the vessel, and one ormore slag ports at the bottom of the carbonaceous bed for exit of moltenand vitreous material from the vessel; and additional inlets through theside wall of the reactor vessel for injection of carbon fines into thecarbonaceous bed wherein the additional inlets include at least oneinlet that is arranged to receive carbon fines from an arrangement thatincludes an eductor receiving a carrier gas of solids at a firstpressure and a pressurized gas at the second, higher, pressure injectingsolids from the first gas into the carbonaceous bed.
 15. The apparatusof claim 14, wherein: the additional inlets further comprise a nozzleconfigured to inject air, oxygen and/or steam into the carbonaceous bed.16. The apparatus of claim 14, wherein the carbonaceous bed comprisesbricks that contain carbon and are of varied size and shape of which atleast 25% of the total carbon content of the bed comprises spent potliner material from aluminum processing, and wherein the bricks furthercomprise at least one of: Portland cement, potassium silicate cement, oraluminum silicate cement.
 17. The apparatus of claim 16, wherein thebricks further comprise one or more of: bentonite clay, sand, sodiumsilicate, and aluminum hydroxide.
 18. The apparatus of claim 14, whereinthe carbonaceous bed comprises bricks that contain carbon and are ofvaried size and shape of which at least 25% of the total carbon contentof the bed comprises soot water residue from a gasification reactor, andwherein the bricks further comprise at least one of: Portland cement,potassium silicate cement, or aluminum silicate cement.
 19. Theapparatus of claim 18, wherein the bricks further comprise one or moreof: bentonite clay, sand, sodium silicate, and aluminum hydroxide.